US4025321A - Purification of natural gas streams containing oxygen - Google Patents
Purification of natural gas streams containing oxygen Download PDFInfo
- Publication number
- US4025321A US4025321A US05/618,062 US61806275A US4025321A US 4025321 A US4025321 A US 4025321A US 61806275 A US61806275 A US 61806275A US 4025321 A US4025321 A US 4025321A
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- US
- United States
- Prior art keywords
- bed
- oxygen
- feedstock
- hydrocarbon
- impurity
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 0 CC*C(C)C(*)C1C(CN)CCC1 Chemical compound CC*C(C)C(*)C1C(CN)CCC1 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
- C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/104—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/06—Polluted air
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/403—Further details for adsorption processes and devices using three beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/41—Further details for adsorption processes and devices using plural beds of the same adsorbent in series
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Definitions
- the present invention relates in general to the purification of hydrocarbon fluid streams and more particularly to the purification of hydrocarbon fluid streams which contain from 10 ppm to 10,000 ppm oxygen impurity in addition to one or more other impurities such as water, carbon dioxide and sulfur compounds.
- the adsorption process utilizes one or more fixed beds of molecular sieve adsorbent through which the feedstock is passed and the impurity is retained. Flow-through of the feedstock is terminated before breakthrough of the adsorbable impurity and thereafter the bed is regenerated by countercurrent hot purge desorption and subsequent cool-down with a minor portion of the purified product or some other available purge fluid essentially free of sorbable constituents undesirable in the purified feedstock product.
- oxygen is frequently found in relatively small concentrations in either the hydrocarbon feedstocks being purified or in the hydrocarbon purge fluid or in both. Being non-condensible at temperature and pressure conditions used to liquify hydrocarbon gas stream and being essentially non-sorbable on molecular sieves under the conditions prevailing in adsorption purification processes for hydrocarbons, the oxygen present in most hydrocarbons has been largely ignored. It is found, however, that a number of problems can be created by the presence of oxygen in hydrocarbon fluids treated in contact with molecular sieves, even if present in amounts as low as 10 ppm.
- natural gas quite frequently contains some gaseous oxygen, and can contain as much as 10,000 parts per million (volume). Usually amounts greater than 500 ppm are found in natural gas obtained from low pressure or sub-atmospheric pressure gas fields. In pipeline natural gas some oxygen is doubtlessly introducted during pipeline hydrotesting, during in ground, i.e., cavern, storage and during periodic compression along the pipeline.
- oxygen-containing hydrocarbon feedstocks e.g. natural gas
- the oxygen can interfere with the adsorption-purification process in a number of ways, depending on the concentration of the oxygen, the temperature of the adsorption system and the presence of sulfur compounds.
- oxygen reacts appreciably with sulfur compounds such as H 2 S and mercaptans to produce sulfur and water as principal reaction products.
- sulfur compounds such as H 2 S and mercaptans
- These substances are strongly held on the zeolite surfaces and seriously affect the capacity of the adsorbent bed to retain the impurities desired to be removed from the feedstock being treated. Sulfur is especially harmful in this regard.
- sulfur compounds such as H 2 S and mercaptans
- oxygen is still a problem in hydrocarbon feedstocks since it reacts appreciably with hydrocarbons to form water, oxygenated organic compounds and/or carbon dioxide.
- reaction products are, in part, formed in the adsorption bed ahead of the impurities mass transfer zones and are thus to some extent purged from the bed into the purified product stream before the normal termination of the adsorption stroke in the bed. Purity specifications for the product stream are thereby adversely affected.
- adsorption purification processes employ temperatures below 150° F. during the adsorption step, and hence most of the above-mentioned problems are not encountered in that stage of the overall process.
- the purge-desorption step must be accomplished at temperatures at least higher than 150° F. and preferably at temperatures higher than 350° F. in order to avoid the need for unduly large quantities of purge gas.
- the purge gas is a non-sorbable hydrocarbon, such as purified natural gas, and contains from 10 to 10,000 ppm (volume) of O 2 , the aforesaid harmful effects due to the presence of oxygen are encountered.
- a hydrocarbon feedstock containing at least one sorbable impurity selected from the group consisting of water, carbon dioxide, hydrogen sulfide and alkyl mercaptan is passed through a first fixed bed of activated zeolitic molecular sieve having pore diameters large enough to adsorb the said impurity, with the proviso that the said fixed bed is at a temperature of less than 150° F.
- said hydrocarbon feedstock also contains from 10 to 10,000 ppm (volume) of gaseous oxygen, terminating the passage of the feedstock through the bed prior to breakthrough of the impurity adsorbed therein, thereafter desorbing and removing the adsorbed impurity from said first bed by purging same counter-currently with a non-sorbable hydrocarbon purge gas previously containing from 10 to 10,000 ppm by volume of molecular oxygen, said oxygen-containing hydrocarbon purge gas stream having been treated by the steps of (a) reducing the elemental oxygen content thereof by reacting the oxygen with hydrocarbon molecules comprising the said gas stream, preferably by heterogeneous catalysis in contact with an oxygenation catalyst mass in the solid state, and (b) passing the oxygen-depleted hydrocarbon gas stream together with at least some of the oxygen-containing reaction products produced in situ therein through a second fixed bed of activated zeolitic molecular sieve adsorbent, the temperature of the gas stream being less than 350° F., preferably less than 150° F. and said molecular
- the species of molecular sieve adsorbent employed in the adsorbent beds of the present process are well known in the art and are not critical factors. It is necessary only that the pores of the adsorbent are large enough to adsorb the impurity components of the feedstock hydrocarbon being treated and the oxygen-containing reaction products produced in the purge gas stream.
- the calcium form of zeolite A described in detail in U.S. Pat. No. 2,882,243, has a high capacity for the adsorption of water and carbon dioxide and is advantageously employed.
- the hydrocarbon feedstock treated can be any of those commonly involved in petroleum refining operations and in some aspects of petroleum production. Natural gas streams are ideally suited for treatment by the present process.
- the feedstock In the purification-adsorption step of the process the feedstock can be in the liquid or in the vapor state.
- the hydrocarbon gas stream which is treated so that it can be used to hot purge desorb the impurity-laden adsorbent can be any oxygen-containing hydrocarbon stream in which the principal hydrocarbons are non-sorbable, i.e. are less strongly adsorbed in the inner adsorption cavities of the molecular sieve adsorbent than the least strongly adsorbed impurity to be removed from the feedstock being purified.
- molecules which are excluded from the inner adsorption cavities of a molecular sieve species by virtue of the pore diameters of thereof are considered to be less strongly sorbable on that zeolite species than smaller molecules which can pass through the zeolite pores even though the larger molecules may be more strongly held than the smaller ones in zeolites having pores large enough to adsorb both molecular species.
- methane, ethane and n-butane can be used to purge CO 2 impurity from a zeolite adsorbent having pore diameters not greater than 4 Angstroms
- methane, ethane and iso-butane can be used to purge CO 2 from a molecular sieve having pore diameters of 5 Angstroms or less.
- Large concentrations of hydrogen, nitrogen and inert gases can be tolerated in the purge gas stream.
- the purge gas will be natural gas from which the water, carbon dioxide and sulfur compounds have been removed, or a comparable gas stream consisting essentially of methane.
- the present invention not only converts an unsuitable purge gas stream to an entirely satisfactory one, but also in the treatment of the gas stream there is provided the added advantage that a hot previously regenerated adsorbent bed is cooled down to adsorption stroke temperature and much of the heat energy therefrom is transferred to the purge desorbing of another bed using the newly purified purge gas stream.
- a natural gas feedstock (a) containing at least one sorbable impurity selected from water, carbon dioxide, hydrogen sulfide and alkyl mercaptan, and containing as a non-sorbable impurity from 10 to 10,000 ppm (volume) of entrained oxygen is passed at a temperature below 150° F.
- FIGURE is a schematic flow diagram of a three-bed adsorption purification system in which each of the three beds cyclically undergoes the steps of adsorption, countercurrent hot purge desorption and co-current cool down. Operation of the process is such that at any given time all three steps are in progress with each step being carried out in a different bed.
- the conventional valving and conduit connections which enables cycling of the process steps in each bed are not shown in the drawings.
- Natural gas which contains 1.5 volume-% carbon dioxide and 150 ppm (volume) H 2 O and 50 ppm (volume) oxygen is purified in an adsorption system comprising three fixed adsorption beds, each containing 35,000 pounds of type 4A molecular sieve.
- the natural gas feedstock is passed at the rate 32.5 million standard cubic feet per day through line 10 at a temperature of 85° F. and at a pressure of 600 psi.
- carbon dioxide and water are adsorbed and the effluent product gas stream through line 14 contains less than 50 ppm CO 2 , less than 1 ppm H 2 O and essentially the same concentration entrained oxygen present in the feedstock.
- a slipstream of product gas is removed from line 14 via line 16 at the rate of 17.4 million standard cubic feet per day, heated to 400° F. in furnace 18 and passed through line 20 to catalytic oxidation unit 22.
- the catalyst mass in unit 22 consists of cuprous oxide dispersed on synthetic mordenite having an SiO 2 /Al 2 O 3 molar ratio of 11.2, and converts sufficient oxygen of the gas stream to CO 2 and H 2 O to lower the entrained oxygen content to less than 10 ppm (volume).
- the effluent gas stream carrying the product CO 2 and H 2 O is passed via line 24 through cooler 26 wherein the temperature of the effluent is reduced to about 100° F. and thereafter is fed through line 28 into adsorption bed 30.
- Bed 30 had been utilized to purify a portion of the same feedstock as currently is being treated in bed 12.
- Bed 30 has also been hot purge desorbed at a temperature of 500° F. in a direction counter-current to the flow of the feedstock stream and the cooling oxygen-depleted gas stream currently flowing through line 28.
- the gas stream from cooler 26 through line 28 deposits CO 2 and H 2 O as adsorbates on the ingress end of the bed in a well defined adsorption zone, cools the bed 30 along an advancing cold front, and is itself heated to approximately 500° F.
- This effluent hot, dry and essentially CO 2 -free gas stream is passed via line 32 to furnace 34, wherein it is heated to 600° F.
- Bed 40 has previously been employed to purify, in a direction counter-current to the direction of flow of the present gas stream, a portion of the same feedstock as is currently being treated in bed 12, and is loaded with adsorbed CO 2 and H 2 O impurities. Bed 40 is regenerated and heated by the passage therethrough of the purging gas stream from line 36 and the desorbed CO 2 and H 2 O is passed through line 42 for disposal.
Abstract
Description
Claims (5)
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US05/618,062 US4025321A (en) | 1975-09-30 | 1975-09-30 | Purification of natural gas streams containing oxygen |
NL7613241A NL7613241A (en) | 1975-09-30 | 1976-11-26 | PURIFICATION OF OXYGEN CONTAINING NATURAL GAS FLOWS. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US05/618,062 US4025321A (en) | 1975-09-30 | 1975-09-30 | Purification of natural gas streams containing oxygen |
NL7613241A NL7613241A (en) | 1975-09-30 | 1976-11-26 | PURIFICATION OF OXYGEN CONTAINING NATURAL GAS FLOWS. |
Publications (1)
Publication Number | Publication Date |
---|---|
US4025321A true US4025321A (en) | 1977-05-24 |
Family
ID=26645262
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US05/618,062 Expired - Lifetime US4025321A (en) | 1975-09-30 | 1975-09-30 | Purification of natural gas streams containing oxygen |
Country Status (2)
Country | Link |
---|---|
US (1) | US4025321A (en) |
NL (1) | NL7613241A (en) |
Cited By (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4137054A (en) * | 1976-01-22 | 1979-01-30 | Asahi Kasei Kogyo Kabushiki Kaisha | Purification of formaldehyde by separation |
JPS58190801A (en) * | 1982-04-28 | 1983-11-07 | Kansai Coke & Chem Co Ltd | Method for recovering high purity hydrogen from coke oven gas |
US4425143A (en) | 1978-12-29 | 1984-01-10 | Shin Tohoku Chemical Industries Inc. | Adsorption by zeolitic composition |
US4449991A (en) * | 1982-12-20 | 1984-05-22 | Exxon Research And Engineering Co. | Removal of sulfur from process streams |
US4498910A (en) * | 1981-12-18 | 1985-02-12 | Linde Aktiengesellschaft | Safe adsorption process for the separation of hydrocarbons from oxygen containing gas |
EP0178833A2 (en) * | 1984-10-18 | 1986-04-23 | Imperial Chemical Industries Plc | Gas recovery |
EP0203408A2 (en) * | 1985-05-30 | 1986-12-03 | Linde Aktiengesellschaft | Process for cleaning a gas stream containing oxygen and sulfur compounds |
US5089034A (en) * | 1990-11-13 | 1992-02-18 | Uop | Process for purifying natural gas |
EP0708679A1 (en) * | 1993-07-15 | 1996-05-01 | Richard F. Sowinski | Gas stream odorant filtering apparatus and method |
US6495112B2 (en) * | 2001-03-16 | 2002-12-17 | Phillips Petroleum Company | Method and apparatus for removing oxygen from natural gas |
US20040261617A1 (en) * | 2003-06-30 | 2004-12-30 | Stewart Albert E. | Methods and systems for pressure swing regeneration for hydrogen generation |
US20050220704A1 (en) * | 2004-03-30 | 2005-10-06 | Morrow Jeffrey M | Method of storing and supplying hydrogen to a pipeline |
WO2006076096A1 (en) * | 2005-01-11 | 2006-07-20 | Univation Technologies, Llc | Feed purification at ambient temperature |
US20070017852A1 (en) * | 2005-03-08 | 2007-01-25 | Peter Meyer | Process of removal of sulphur compounds from hydrocarbon streams using adsorbents |
US20100000251A1 (en) * | 2006-07-13 | 2010-01-07 | Michiel Gijsbert Van Aken | Method and apparatus for liquefying a hydrocarbon stream |
CN101098897B (en) * | 2005-01-11 | 2010-05-26 | 尤尼威蒂恩技术有限公司 | Feed purification at ambient temperature |
US20100261856A1 (en) * | 2007-11-15 | 2010-10-14 | Univation Technologies, Llc | Methods for the removal of impurities from polymerization feed streams |
US20110027156A1 (en) * | 2008-04-17 | 2011-02-03 | Univation Technologies, Llc | Systems and Methods for Removing Impurities From a Feed Fluid |
US8425149B2 (en) | 2010-06-10 | 2013-04-23 | Praxair Technology, Inc. | Hydrogen storage method and system |
US20130180282A1 (en) * | 2012-01-12 | 2013-07-18 | Gary Palmer | Simplified LNG Process |
US8690476B2 (en) | 2012-05-25 | 2014-04-08 | Praxair Technology, Inc. | Method and system for storing hydrogen in a salt cavern with a permeation barrier |
US8950419B2 (en) | 2012-02-16 | 2015-02-10 | Praxair Technology, Inc. | Hydrogen supply method and system |
US9284120B2 (en) | 2012-05-25 | 2016-03-15 | Praxair Technology, Inc. | Methods for storing hydrogen in a salt cavern with a permeation barrier |
US9707603B2 (en) | 2014-09-30 | 2017-07-18 | Praxair Technology, Inc. | System and method for purging contaminants from a salt cavern |
US9718618B2 (en) | 2014-09-02 | 2017-08-01 | Praxair Technology, Inc. | System and method for treating hydrogen to be stored in a salt cavern and supplying therefrom |
US9950927B2 (en) | 2015-12-18 | 2018-04-24 | Praxair Technology, Inc. | Method of supplying hydrogen through an integrated supply system |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2924504A (en) * | 1956-08-30 | 1960-02-09 | Chemetron Corp | Process of removing nitrogen oxides from gas streams of varying composition |
US3023841A (en) * | 1957-10-22 | 1962-03-06 | Union Carbide Corp | Desorption of oxygen-contaminated molecular sieves |
US3094569A (en) * | 1958-10-20 | 1963-06-18 | Union Carbide Corp | Adsorptive separation process |
US3841058A (en) * | 1972-03-03 | 1974-10-15 | British Gas Corp | Method for the purification of natural gas |
US3864452A (en) * | 1972-03-30 | 1975-02-04 | Grace W R & Co | Process for purifying sulfur compound contaminated gas streams |
-
1975
- 1975-09-30 US US05/618,062 patent/US4025321A/en not_active Expired - Lifetime
-
1976
- 1976-11-26 NL NL7613241A patent/NL7613241A/en active Search and Examination
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2924504A (en) * | 1956-08-30 | 1960-02-09 | Chemetron Corp | Process of removing nitrogen oxides from gas streams of varying composition |
US3023841A (en) * | 1957-10-22 | 1962-03-06 | Union Carbide Corp | Desorption of oxygen-contaminated molecular sieves |
US3094569A (en) * | 1958-10-20 | 1963-06-18 | Union Carbide Corp | Adsorptive separation process |
US3841058A (en) * | 1972-03-03 | 1974-10-15 | British Gas Corp | Method for the purification of natural gas |
US3864452A (en) * | 1972-03-30 | 1975-02-04 | Grace W R & Co | Process for purifying sulfur compound contaminated gas streams |
Cited By (44)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4285811A (en) * | 1976-01-22 | 1981-08-25 | Asahi Kasei Kogyo Kabushiki Kaisha | Purification of formaldehyde by separation |
US4137054A (en) * | 1976-01-22 | 1979-01-30 | Asahi Kasei Kogyo Kabushiki Kaisha | Purification of formaldehyde by separation |
US4425143A (en) | 1978-12-29 | 1984-01-10 | Shin Tohoku Chemical Industries Inc. | Adsorption by zeolitic composition |
US4498910A (en) * | 1981-12-18 | 1985-02-12 | Linde Aktiengesellschaft | Safe adsorption process for the separation of hydrocarbons from oxygen containing gas |
JPS58190801A (en) * | 1982-04-28 | 1983-11-07 | Kansai Coke & Chem Co Ltd | Method for recovering high purity hydrogen from coke oven gas |
JPS618002B2 (en) * | 1982-04-28 | 1986-03-11 | Kansai Netsukagaku Kk | |
US4449991A (en) * | 1982-12-20 | 1984-05-22 | Exxon Research And Engineering Co. | Removal of sulfur from process streams |
AU571355B2 (en) * | 1984-10-18 | 1988-04-14 | Imperial Chemical Industries Plc | Pressure swing adsorption of carbon monoxide |
EP0178833A2 (en) * | 1984-10-18 | 1986-04-23 | Imperial Chemical Industries Plc | Gas recovery |
EP0178833A3 (en) * | 1984-10-18 | 1987-01-14 | Imperial Chemical Industries Plc | Gas recovery |
EP0203408A3 (en) * | 1985-05-30 | 1987-01-28 | Linde Aktiengesellschaft | Process for cleaning a gas stream containing oxygen and sulfur compounds |
EP0203408A2 (en) * | 1985-05-30 | 1986-12-03 | Linde Aktiengesellschaft | Process for cleaning a gas stream containing oxygen and sulfur compounds |
US5089034A (en) * | 1990-11-13 | 1992-02-18 | Uop | Process for purifying natural gas |
EP0708679A1 (en) * | 1993-07-15 | 1996-05-01 | Richard F. Sowinski | Gas stream odorant filtering apparatus and method |
EP0708679A4 (en) * | 1993-07-15 | 1997-01-22 | Richard F Sowinski | Gas stream odorant filtering apparatus and method |
US6495112B2 (en) * | 2001-03-16 | 2002-12-17 | Phillips Petroleum Company | Method and apparatus for removing oxygen from natural gas |
US20040261617A1 (en) * | 2003-06-30 | 2004-12-30 | Stewart Albert E. | Methods and systems for pressure swing regeneration for hydrogen generation |
US6942719B2 (en) * | 2003-06-30 | 2005-09-13 | The Boeing Company | Methods and systems for pressure swing regeneration for hydrogen generation |
US20050220704A1 (en) * | 2004-03-30 | 2005-10-06 | Morrow Jeffrey M | Method of storing and supplying hydrogen to a pipeline |
US7078011B2 (en) * | 2004-03-30 | 2006-07-18 | Praxair Technology, Inc. | Method of storing and supplying hydrogen to a pipeline |
CN101098897B (en) * | 2005-01-11 | 2010-05-26 | 尤尼威蒂恩技术有限公司 | Feed purification at ambient temperature |
WO2006076096A1 (en) * | 2005-01-11 | 2006-07-20 | Univation Technologies, Llc | Feed purification at ambient temperature |
US20070017852A1 (en) * | 2005-03-08 | 2007-01-25 | Peter Meyer | Process of removal of sulphur compounds from hydrocarbon streams using adsorbents |
US20100000251A1 (en) * | 2006-07-13 | 2010-01-07 | Michiel Gijsbert Van Aken | Method and apparatus for liquefying a hydrocarbon stream |
US20100261856A1 (en) * | 2007-11-15 | 2010-10-14 | Univation Technologies, Llc | Methods for the removal of impurities from polymerization feed streams |
US9133081B2 (en) | 2007-11-15 | 2015-09-15 | Univation Technologies, Llc | Methods for the removal of impurities from polymerization feed streams |
US8852541B2 (en) | 2008-04-17 | 2014-10-07 | Univation Technologies, Llc | Systems and methods for removing impurities from a feed fluid |
US20110027156A1 (en) * | 2008-04-17 | 2011-02-03 | Univation Technologies, Llc | Systems and Methods for Removing Impurities From a Feed Fluid |
US9278807B2 (en) | 2010-06-10 | 2016-03-08 | Praxair Technology, Inc. | Hydrogen storage method and system |
US8757926B2 (en) | 2010-06-10 | 2014-06-24 | Praxair Technology, Inc. | Hydrogen storage method and system |
US10017324B2 (en) | 2010-06-10 | 2018-07-10 | Praxair Technology, Inc. | Hydrogen storage method and system |
US8425149B2 (en) | 2010-06-10 | 2013-04-23 | Praxair Technology, Inc. | Hydrogen storage method and system |
US20130180282A1 (en) * | 2012-01-12 | 2013-07-18 | Gary Palmer | Simplified LNG Process |
US9612050B2 (en) * | 2012-01-12 | 2017-04-04 | 9052151 Canada Corporation | Simplified LNG process |
US8950419B2 (en) | 2012-02-16 | 2015-02-10 | Praxair Technology, Inc. | Hydrogen supply method and system |
US9651199B1 (en) | 2012-02-16 | 2017-05-16 | Praxair Technology, Inc. | Hydrogen supply method and system |
US9574715B2 (en) | 2012-02-16 | 2017-02-21 | Praxair Technology, Inc. | Hydrogen supply method and system |
US9284120B2 (en) | 2012-05-25 | 2016-03-15 | Praxair Technology, Inc. | Methods for storing hydrogen in a salt cavern with a permeation barrier |
US8690476B2 (en) | 2012-05-25 | 2014-04-08 | Praxair Technology, Inc. | Method and system for storing hydrogen in a salt cavern with a permeation barrier |
US10173840B2 (en) | 2012-05-25 | 2019-01-08 | Praxair Technology, Inc. | System for operating a hydrogen storage salt cavern |
US10315846B2 (en) | 2012-05-25 | 2019-06-11 | Praxair Technology, Inc. | Methods for storing hydrogen in a salt cavern |
US9718618B2 (en) | 2014-09-02 | 2017-08-01 | Praxair Technology, Inc. | System and method for treating hydrogen to be stored in a salt cavern and supplying therefrom |
US9707603B2 (en) | 2014-09-30 | 2017-07-18 | Praxair Technology, Inc. | System and method for purging contaminants from a salt cavern |
US9950927B2 (en) | 2015-12-18 | 2018-04-24 | Praxair Technology, Inc. | Method of supplying hydrogen through an integrated supply system |
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